Pipelining crude oil



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Filed Jan. 3. 1966 Y 5 Sheets-Sheet 2 PRESSURE DROP IN 3 INCH PIPE CASMALIA EMULSIONS HARLEY f.- JENNING$,JR.

f fan. e, wf@ www am rrreunma cnuns on.

rma Jan. 1966 s shuts-Shen 4 PRESSURE DROP mi a.' mol-l MPE o su/so o/w eMuLsloNs 5 7005 A 800K so D i 1 l l l u l I f 5 1 2 0 Y 'GAL/Mm.

,MAMA

FIGA

l INVENTORS 'RALPH smo/ 4 -cLArToN o. uuu/.irrt ,wEsLsr G. Por/vrfn HARLEY r. JENA/1116s,@

3,487,844 PIPELINING CRUDE OIL 'dsa-tes harem n Ralph Simon, Whittier, ClaytnnD..McAulie, Fullerton,

Wesley G. Poynter, Whittier, and Harley Y. Jennings, Y

Jr., Fullerton, Calif., seniors to Chevron Research Company, San -Franuscg Calif., a corporation of Delaware Filed Jan. 3, 1966, er. No. 518,124 Int. Cl. Flld .I/I U-S. Cl. 131-13 14 Claims ABSTRACT 0F TEE DISCLOSURE A method of transporting visons crude oils by pipeline wherein water containing a base such as sodium hydroxide is mixed with the crude oil in the presence of an emulsifying agent so as to form an uil-in-water emulsion thereby facilitating the movement of the oil through the pipe.

This invention is directed to transporting viscous crude oils; and, more particular.'- this inventief: is directed t0 methods of transporting viscous crude oils ."rough pipelines in emulsiiied form.

There are many crude oils that are extremely viscous when produced and are thus quite ditlcult to transport.

K One 'of' the methods usedheretofore to transport such oils d l' assists Patented Jan. s, 1910 containing about 50 to 70 percent oil and 50 to 30 per- 4 cent water by volume based on the emulsion.

In this regard, it is contemplated that, for a particular crude oil that is desired to transport, lab tests will be done and the optimum concentration and amount of the basic solution will be determined. It is necessary that the concentration of the basic solution be adiusted to within a relatively narrow range, since if the concentration is too low emulsiiication will not occur or will be incoluplete and if thev concentration is too high inversion of the emulsion from oil-in-water to water-in-oil will cccur with the resulting prohibitive increase in viscosity which may be higher even than the original viscosity nf the oil.

The base used in forming the aqueous alkaline solution can be a metal alkaline hydroxide, such as sodium hydroxide, potassium hydroxide, and lithium hydroxide orammonium hydroxide. In addition to the inorganic bases, it is also possible to use strong organic bases, such as the amines-for example, ethylamine, propylamine, tricthawas shipping heated batch quantities, such as by truck. l

Various methods of pipclining extremely viscous crudes .have also been attempted. The viscosities of the crudes so pipelined were reduced by adding a dilucnt to the viscous crude or by means of heating the oil bctore passing it. through a pipeline. Since these methods are relutively expensive, the need for an inexpensive method of transporting viscous crudcs is still required.

In accordance with the invention, it has been found that the viscosity of crude oils can be greatly reduced by contacting the crude with water and a base in the presence of an emulsifying agent for the viscous crude. By

Y suitably agitating the crude and aqueous basic solution,

an oil-in-water emulsion is formed. This oil-in-water emulsion is then moved through a pipeline. At a suitabie location at the downstream end of the pipeline an emulsion breaking agent is added to the emulsion. The oil and y water are separated for further use.

In. general, the oil-in-water emulsions of the invention contain by volume about 50 to 70 percent oil and 30 to percent water based on the emuison. The aqueous continuous phase of the emulsion contains the base in a concentration within about the range 0.002 N and 0.75 N. The viscosity of the emulsion can be varied by adjusting its water content, the viscosity being lower with increased water content and increased by raising the oil content.

The invention is particularly useful when applied to asphaltic etudes-for examples, the heavy California crudos-which, upon contact and agitation with a suitable aqueous basic solution, are convened into an oi1-in-water emulsion. Accordingly, it has been found that the viscosity of the crude can be reduced by a factor of 100 to 1,000 that of the original viscous asphaltc crude by adding to the crude an aqueous solution of a base-for example, sodium hydroxide-to react with the saponiable consu'tuents of the crude to produce an oil-in-water emulsion. As hereinabove mentioned, the amount and con eentratcn of the base solution for mixing with the crude may range in concentration from about 0.002 N to l N or higher and is such that the concentration of the base upon creation of the emulsion is in about the range 0.002 N to 0.75 N based on the total water present after emull-f sification; that is, the water not only contributed by the alkaline solution but also any connate water present in the oil that Vis to be emulsied to produce an emulsion nolamine--thus forming emulsifyin g amine soaps with the acid contained in the asphaltic group. Generally, because of cost, it is preferred to use a causc solution formed of sodium hydroxide.

As mentioned, the invention is particularly useful when applied to asphaltic crudes that contain saponiliable constituents capable. of forming with the .,base. solution ctcctive emulsifying agent required in forming the oilin-water emulsion. Examples oi' such crude oils are the naphthenic base crude oils, such as the heavy California crude oils, for example, those of the Valley" (Kern County, Coalinga) and coastal crudes (Santa Maria); the

heavy Venezuelan crudos, for example, Boscan; the heavy Mexican crudes, for example, the Ebano and Panuco type; the heavy crude oils of the Texas GulfCoast; the asphaltic-containing crudes in Mississippi; the naphthenic oil from the Mid-Continent Feids.

Various crude oils have different susccptibiliti to form the desired oil-in-water emulsions required to obtain the benefit of the present invention. Specifically, it is desirable toevaluate the crude oil for its ability to form the desired emulsion prier, to mixing sodium hydroxide or other alkali metal hydroxide solutions with the crude to form the prescribed oil-in-water emulsion. Taking mdium hydroxide as representative, several examples of crude oils will be given below to indicate suitabie concentration ranges to form a desirable oil-n-water emulsion. Generally, the emulsions are most readily formed by crude oils having high acid numbers. The emulsion is also more easily formed with fresh waters whose salt content islow. If the native or connate water from the formations producing oil has a high salt content, it is sometimes necessary either to supply greater quantities of fresh water from the surface or to remove some of the connate water from the oil.

Table 1 illustrates etective langes of sodium hydroxide in weight percent concentration in the aqueous phase that have been used to emulsify samples of crude oil to form oil-in-water emulsions. The dcontinncns cil phase was maintained at about 10 percent by volume to produce oil-inwater emulsions.from crude oils over the given preferred ranges.

TABLE l Cat Canyon 0.1-4.0

NaOH conc., Wt.

annate 'i are certain oil-bearings formations in which the formation water has a sufliciently high alkali metal carborn content to permit formation of alkali metal hydroxide when mixed with an alkaline earth metal hydroxide, such as calcium hydroxide, a relatively les expensive alkaline material, which reacts with the connate water to form ir.- soluble alkaline earth metal carbonate and aqueous alkali metal hydroxide.

For example, in the Boscan leld in Venezuela, formation water has a high. sodium bicarbonate contertcalcium hydroxide is locally availabk and inexpensivewhle sodium hydroxide must be imported. The invention can be practiced in the Boscan field by mixing eitifer a saturated solution of calcium hydroxide or a dilute sperson of solid calcium hydroxide in water with the formation wa er to cause reaction-forming calcium car bonate precipitate and dilute aqueous sodium hydroxide which, when mixed with the oil, will cause the formation of an oil-inwater emulsion in accordance with the invention.

It is also advantageous with water that contains caldi: or magnesium salts to addsodium carbonate along with the alkali metal hydroxide to form calcium carbonate or magnesium hydroxide. Even when these compounds do not form a precipitate, they are sufficiently inactivated so that they do not interfere with the reaction of the basic solution with the crude to form an oil-inmate:

emulsion. s t With nonasphaltic etudes-for example, Minas am! Red Wash crudes-that are nevertheless viscous because of the high paraliin content 'out contain little, if any, saponiiiable material, it is possible to form the required oilin-water emulsion by mixing a preformed cmulsifyng agent together with suticient alkaline solution and the nonasphaltic crude. A suitable emulsifying agent can be obtained by extraction of certain lowgravity asphaltiz crndes, such as those produced from numerous forma in California oil fields-for example, Cnsmalia, Sax: Artic, Midway-Sunset, West Coalinga and Poso Creek. lt is also in accordance with the invention in situations where it is desired to -pipeline both an asphaltic crude which wi!! emulsify and a crude which will not emulsify upon the addition of a basic solution to mix the crudas in a pledetermned proportion and then add the basic soluti to the mixture to form an oil-in-water emulsion having desirable properties for pipelining.

The resulting low-viscosity, oil-in water emulsion is stable and can be pumped through a pipeline over a long distance. When the emulsion arrives at a relinery er tanker loading terminal, for example, the emulsion is broken and the water is separated from the oil. Since most reneries have an upper limit of 3 to 6 percent connate water in the delivered oil, it is necessary to pmvide an i4 inexpensive and eicient method of hreakinggtln emulsion andaeparatingtheoilandwatenlnacrdance wth -A the present invention, a salt scintiou is used under controlled conditions of temperature to break the emulsion in an eliicient and inexpensive manner.

Further objects and advantages of the present invention will become apparent from the foilowing detailed deacripton read in view of the accompanying drawings which-are made a part of this specitication, and in which:

FIGURE l is a flow diagram illustrating the preferred embodiment of the present invention;

FIGURE 2 is a chart illustrating the pressure drop in a pipeline when pnmp'mg an emulsion in accordance with the invention;

FIGURE 3 is a chart comparing the dow properties of an emulsion formed in accordance with the invention with a theoretical Suid; Y

FIGURE 4 is a chart illustrating the prescrire dr'op in a pipeline when pumping an emulsion in accordance with the invention;

FIGURES 5a, 5b and 5c are charts illustrating data developed iu breaking an emulsion in accordance with the-invention;

FIGURES Q1, 65 and 6c are charts illustrating data developed in breakingan emulsion in accordance with Lbe invention; and

FIGURES 7a, 7b and 1e are charts illustrating data developed in breaking an emulsion in accordance with the invention. t

FIGURE l `is `a dow diagram illustratingthepreferred embodiment of the present invention. The 0:1 removed frmn the ground is tiowed to a stock tank which is normally used 1n oil field operations to temporarily store oil coming from the wells. In many instances, the oil coming from the wells will be heated by means of a heater trotter',` such as illustrated at 22, to reduce the comme water content of the produced oil and to allow the A oil to dow more rcadih'. In this regard, depending on the comme water content of a particular oil and the properties of the connatc water, it may or may not be necessary or desirable to heat the produced oil to remove contrate Irrel'. s

. A water tank 24 for supplying water for use in preparmg an emulsion in accordance with the present invention is connected by suitable piping for mixing with oil from the `wk tank. The relative freshness of the water which may be needed for use in forming a suitable oilin-water emulsion depends or. the particular oil to be emuisitied and the amount of formation waterincluded with the oil. In certain oils, a water having very low salt content is required for proper emulsicaion. In other oils, salt water or even coprodud water can be used to form the emulsion. Table 2 illustrates the range of arxicm hydroxide concentration and percent of coprodmed water useful in emulsilition of Santa Maria Valiey crude oils.

Y n i vm CRUDE oms ATZREHULSIONS .YIIH SLTA AARIA Percent NaOH wed in Water Phase .A ses essere rata L wen remi wam i-:muxsmns Canali Calrrrallsl'ee.-.-... l: 6.8 0.2-0.5 Do.- -Qw.. 0-.--..:-.....- 2l l 0. 2-0. 3 Stock .lan 1.8 M15-0. 5 a. Penn s. n' tra comme. Harbordr--'.`.1`.`.l. sr 1.1 t2-11g Do.- Williams Holdirrl-.- p 3.8, lll-1.0 Do- G.w r--....-..-.... um r5.7 na-o s uns Alam Getty-B 2 .9 t) Za.--... C lirr.-....... l2 m4 (l) D6.- l 19.0 0. 1-0. 2

mmttittwwcnmumraammr Suitable pumps 26 and 2u, respectively, are used to ow the water and oil through lines 30 and 32 to a proportional iiow control device 34 which utilizes suitable valves and 38 to provide for tlow of predetermined amounts ot oil ,and water in a common mixing line 40. Prior to mixing the water with the oil, a predetermined amount of brac-for example, sodium hydroxide-from a suitable source 42 is mixed with the water. A metering pump 44 is used to more the sodium hydroxide 'through line 46. A proportional ow control means 48 adjusts the ow of water and base through suitable valves 50 and essieu i v 3 known chcmicas are also available. The treating chem- 52 on lines $2 and 46. A e mixer 54 is user?. te insure the proper mixing of the caustic and water prior to owing it into mixing line 40. Downstream of the .cil and basic solution. mixing point, power mixers 56 are l.used to mix the basic solutions and oil to create an oil-n-..'ater emulsion having desirable prorties and viscosity. A viscosity high level alarm instrument 85 may be positioned in the line downstream of mixers 56 to sense and control undesimbly high oil-in-water viscosities. As indicatedV above, it is. of critical importance to maintain the basic y solutions within limits because too little base will result in incomplete cmulsilication While too much base will cause inversion of the emulsion with an attendant increase n viscosity.

lhe suitably prepared emulsion is now moved by pipeline pumps i0 through any desirable length of pipel'ne indicated at 'e2 to emulsion storage tank 64 at the downstream end'of the pipciine. Any number of pipeline pumps such as lpump 60, may be used since the emulsion prepared in accordance with the present invention is stable and not arected 'oy repetitive pumping. FIGURES 2-4 show properties of emulsion formed in accordance with the present invention during movement through pipelines. Specifically, FIGURE 2 hasv a number of curves relating pressure drop to ow rate for emulsions of Casmalia crude. The various emulsions were formed by ufng from 0.10 percent to 0.15 percent sodium hydroxide based on total water. The emulsions were aged as indicated to demonstrate that the emulsions are still easily pumpable alter periods ofinactivty. FIGURE 3 illustrates the flow properties of a number of Gasrnaiia ol-in-water emuisicns and compares them to a theoretical cs. Newtonian lluid. FIGURE 4 illustrates the effect of temperature or. tlow rate and pressure drop for a Casmalia oil-in-water emulsion.

Again referring :o FIGURE 1, it is effen werden to break the oil-in-water emulsion and to separate the oil from the water before moving the oil from the emulsion storage tank 64 to a reli'nery c-r to a ship. 'in this regard, the upper limit for the water content in the oil is usually y set from about 3 to 6 percent by weight. In accordance with the preferred form of the invention, the oil-in-water is moved from the emulsion storage tank 64 by means of pump 66 through lines 68 and 70 to heat exchanger 72 for preheating. The oil is preheated to a temperature above about 200 F. and preferably above 220 F. Ihc heating duid for heat exchange: I2 in the embodiment illus trated is supplied through line 74 and is the bot etiluent from a suitable heater treater 76. The hot oil-in-watel emulsion is then moved thrcugh line 78 and is mixed with salt waterentering the system through pump 80 and line 82, Saline solutions having a dissolved solids content of from 15,000 to 40,000 p.p.m. may be used. In accordical is preferably used in the 'amount of about l gallon per 100 barrels of treated fluid. Power mixers 94, locaued downstream in line 33, provide complete mixing of the emulsion and treated seawater prior to tlowing the mixture into the heater treater 76. In the heater treater 76,

the mixture is heated under pressure to promote the complete separation of oil from water.

A suitable heating source, such as steam unit 96, is useful to raise the temperature in the heater treater to above 250 F. and preferably to above 275 F. The pressure in the heater treater is maintained above 50 p.s.i.g.

' and preferably above 80 p.s.i.g The oil and water separate in the heater treater. The water is tlowed through line 74 to a dotation skimming unit 98 for complete re moval of the oil from the water prior to disposing of the water by means or pump 100 through iter 102. The residual oil from the tlotation skimming unit. is moved from the unit through line 104 by means of pump 106 and is returned to the system through ow line 88. Alternatively, the residual oil, if it meets specication, may

yalso'be piped to "the stock tank." The dil is' removed wvfrom the heater treater 76 through line 86 to a stock tank for use as refinery stock or for further trasportation.

A first demonstration to illustrate the advantages of .this invention-was done yusing Casmalia crude oil which A has a viscosity or' approximately 1,000,000 cs. at 70 F.

Six batches (2S barrels each) of oil-in-water emulsion with different oil/water ratios werf prepared and were circulated through 1,970 feet {equiva 'ent corrected length) of three-inch pipe. The emulsions were made by first loading a tank with an apropriate amount of water and caustic and then adding the oil. Mixing was accomplished by circulating the tank with a pump. All but one o( the emulsion batches were made with Casmalia stock tank ance with the invention, the salt water is-preferably B5 eater haring a dissolved salt content of from about 30,0

150 F. and preferably to above 17S F. in heat exchanger 84 prior to being with the oil-in-water emulsion. The hot fluid is the oil eluent from heater treater 76 and is supplied through line 86.

The seawater and oil-in-water emulsion are mixed in a common mixing line 88 in a ratio of emulsion to seawater of about 3 to l. Emnlsion/seawaterratios of about to about 35.000 p.p.m. The seawater is preheated to above y um* m29S to l to Svi-tol for 601'40 oil-in-water emulsions are 75 oil which had been dried to less than three percent water in -eld heater trfcaters. The remaining. batch included enough connate water to make up 25 percent of the total water.

Data for the runs in the three-inch line are shown in Tabies 3 and 4 and in FIGURE 2. Data are corrected by a viscosity correction factor and compared with a theoretical 10 cs. Newtonian iluid in FIGURE 3. This ligure can be used for line sizing. TheY 50/50 emulsions were very stable and showed no change of properties after five days. The /40 and 65/35 emulsions tended to thicken after several days. This was probably due to insufficient mixing and slight deficicnciex in caustic strength which led to stratification into an oil-rich, oil-in-water emulsion layer over a water-rich, oil-in-water emulsion layer. The

two layers mixed easil,r with only slight agitation, and

stratification did not cause diiculty in starting up a line which had been idle for ten days.

As indicated above, one batch of emulsion or Casmalia crude vas made using a mixture of 25 percent waste water and percent fresh water (all the other batches were triade with fresh water only) to demonstrate the feasibility of disposing of part of the field waste water in the emulsion pipeline process. The emulsion was good and maintained stability. However, 2S percent of the total water is about the maximum permissible waste water content Casmalia crude because its high salt content (15,000 ppm.) prevents proper emulsication in larger proportions.

S TABLE s.-.10MULs1oN 1 1P15LIN1NG (1.4511411111 cntmx om now DATA IN a-I'Ncn 1 rnE LooP Vment Wt. nt 040.111.111 tems AP 11.3.1.1 Q 01111. aged 1011 yummy :"pipa 'pipo 1,000 emulsion emulsion lnwar Temp., F. lncp. f 1w 100D. P51- I. summon/maximin s0 0.10 00 10 00.5 1a. 0.0 0s.: 14.: 1.: 4s.: n.0 a0 1 :1 9 as 2.0

` 'i 'A su 1mm u 1s.s 21.1 12.2

10.. semola u 1a: zu 10.0` v I A 10.4 11.0 0.0 4s.: 0.0 4.0 ma as 1.4

00....---.... 0.10 s1 29 51.5 1x1 1.1 Y .s :as 11.4 f un 21.1 14.0 ss.: 10.4 104 4x0 10.0 .0 i 10.0 u 2.0

v 00 sam nu 141 11.4 10.1v 14a 10.9 11.2 ma 1.9 13.0 .0 40.0 20.: r n.0 2s.: 14.

0s.....'...--........ 0.15 101 41.4 aan :1.4 10.0 13.0 21.0 10.2 j 51.0 as.: 10.8 n.2 14.1. 1.2 11.1 1.0 as a 0.2 1.0

` ss...--.....--..-snyn1d. --1 i '00 A 1d .as :1.0 10.1 fr 31.1 20.0 13.1 21.5 20.0 100 les 14.2 1.2

' l. II. stock 'rank 011.11591, Fxeshwammwamwam l0.. 0.15 05 9.5 11.1 11.0 8.0 Y 1 51.0 1a.; M v 40.5 1.a 0.1 Y '-310 1.a 1.9

-. A -00 20mm n 10 15.0 Y 11.1 as 00.3 V11.4 5.a 40.0 a.: :.3 n.4 as 1.a

Table 4 illustrates a Harbordt lease California clude emulsion was made in two batches of 500 barrels each ppelined in emulsiiied form. The emulsion is a 50/50 and waspumped through 2% miles (13,260 feet) offour- -f I o il-in-wate: emulsion using a .10 percent NaOH in water' inch line. Whenever possible, the emulsions were peras the external phase. The emulsion was slightly lean 55 mitted to stand in the line several days to test stability .v on caustic and partially' suatied but was of generaily under simulated pipeline down conditions. The emulsions good quality and was suitable for emulsion pipelining. were made batchwise by lirst loading a tank with water TABLE 44111111.8101: nrnLmiNG Amami 01mm: on. n.011 nur;

i 1N amen PIPE Loop .i n u vim: we `c Grunn non" m 0H In sOH Viscosity 8" 3" pipe AP NJ] emislcn *1n-.rata Temp., F. in cp. p loop, ps4. 1.0mm

narboratoil/mh wmf I f 0.10 01 u 1&0 :1.0 15.0 01.1 11.0 10.1 1 41.4 1x0 0.1 10.4 ec 4.0

Table 5 illustrates the pipelinug of an emulsied Cascaustie and then adding the oil.. was aecommia crude oil in a four-inch pipeline. 'Ihe oil-n-water 75 Plshed by circulating the tank with a pump.

M. IHN

TABLE 5.-?mi3 PIPELIITNG CABMAIIIA CRUDE OIL FLOW DATA DI LIEGE PIPELINE kse Viscosity Data] Date From- Ferm Vlseomet lleee Remarks C.ps. F.

Sempb No.'

l Castricum... After honrsr mixlng..... 83 91 Kathrein..- After setting over weekend.--- $8 83 1 dn Dug-lng minlnv n 12 4 molly,--. Top oi tank alter standing 85 overnight. s Nortllw tt oitnkth ongh l un s: l. a er o g r line from McNally. p D" 7....... lleNdly.--- After ltriowirlilg through Dipe- 21 93 e on: 8 Nurtham.... After standing overnight a B 83 Gage Readings. psig.

Northam McNally PJJ. PAL/1MB.

a) 1Q 22 1&0 ml 3) 121 9.6 35 m0 211 15.9 141 20 77 5.8

cipal emulsion-breaking agent. Emulsion, seawater and a xxnall amount of treating chemical were mixed together and heated to aint 27S F. The mixture was thoroughly agitated and passed through a small coalescer into a horizontal separator. In many cases, the use of coalescer is not necessary. Dry oil was withdrawn from the top of the separator and tanked. Waste Water from the bottom of .a separator was clarified before disposal by air blowng in a skimming pond and filtering through excelsior pans.

Approximately l50laboratory scale screening tests were made to evaluate diterent emulsion-breaking solutions and to optimize the important process variables. These tests showed that ordinary seawater is effective and more economical than artificially prepared salt or acid solutions. Itv has been fotmd that acid addition, while theoretically desirable to neutralize the caustic emulsiier, is practically undesirable beuse acid causes very rapid demulsitication which tends to enti-ap emulsification water in the oil FIGURES 5-7 illustrate results of these tests. Thorough emulsionfseawater mixing is essential. Satisfactory oil-in- Y water separation requires l to 2 hours residence of the seawaterJemulsion mixture at about 275 F. and the addition of small amounts of treating chemical, such as CHEM-GLENE 476 or other suitabe agent.

Emulsion/seawater ratios of from about 2% to 356 to 1 for 60/40 oil-irrwater emulsions are suitable. An emulsion/seawater ratio of 3 to l is the preferred ratio. Lower ratios than those set out above do not result in complete demulxitcation while higher ratios are not economical and do not produce sgnitcantly better results.

Additional demonstrations were conducted to show the advantages of the present method with various oils. The demonstrationsaresetoutinTable 6.

The emulsion ratio was $0150 clhmter and was prepared a: 150 F. The caustic concentration is set out in the table for each oil. The emulsion breaking was done using seawater in a 2 to 1 ratio with the emulsion at 200 F. A small portion (l part/2,003 parts emulsion) VISCO R-Z-E was added tothe mk-ba nitrati-,emmeloobreaking stage. The water cuts for the etudes after separation are satisfactory. Y

A further demonstration was confirmed to show a method sometimes available as an altermtive to the pre- Y ferred embodiment of the present invention In this demonstration, the emulsion was a 70 percem oi1-inwater emulsion formed by adding an aqneom 0.2 percent sodium hydroxide solution to Casmalia I-4 crude. The emulsion thus formed was suitable for pipeming asdescribed above. The technique used to break the emulg'on included adding l .3 grams of calcium chi-ride 4to each 100 grams of emulsion and bubbling C0, through vtime rcsniting mixture. Two ml. of CO, per minute were buwled through the mixture for approximately four hours. The water cut of the separated oil wasa satisfactory 1.95 percent.

-We claim: y

l. A method of transporting a vcons crude oil from aiirstlocationtoasecondlocaoncom contacting at a rst location a viscous crude oil with water containing betwecn 0.05 and L4 weight percent based on total water of a base in the presence of an emulsifying agent for the viscous crude cil, the ratio of said crude oil to said water being in the range of from between 50/50 to /30, agitating the crude and the war containing said base to form an oil-in-watet emulsion, moving the oil-in-water emulsion through a pipeline from said rst location to a second location, breaking the emulsion at said second location and separaringthecmde oiland'the water.

2. The method ofclaim I fnriherclrmafzridin that the base is sodium hydroxide. th3. 'l'hlthod of claim Ifnrtherdraracrid inthat eem nbreakingspinclndesbubblngCOg through the emulsion.

TABLE .v-DEHNSTRATIONS 0F EMULSION PREPARATION (50150 OIL/WATER RLTIG) EMULSIO?.Y BREAKING WITH SEAWATEB Qilvlse. Water NaOHfor Emulsion an! Gravity at eut em vrssity lrreahxg' Cmd. APf 7% F. percent' wt. pement' ep. d70 F. emulsion 14. 7 637 Trace--- 0. 10 2J- 117 5, 100 ...do..... 0. 12 11 4.!

liiliwimm,

MI" *F 4. A of transporting a viscous crude oil from a rst location to a second location comprising contacting at a first location a viscous crude oil with water containing between 0.05 and 1.4 weight percent based on total water of a base in the presence of an emulsifying agent for the viscous crude oil, agitating the crude and the water containing said -base to form an oil-inwater emulsion, moving the oil-in-water emulsion through a pipeline from said first location to a second location, mixing the emulsion with a saline solution having a. dissolved solids content between 15,000 and 40,000 p.p.m. at a temperature assis@ in excess of 200 F. and in a ratio of emulsion to saline solution of from between 2 to 1 to 3% to 1 to break the emulsion at said second location and separating the crude oil and the water.

5. The method of claim 4 where the base is sodium hydroxide.

6. The method of claim 4 where the saline solution is seawater.

7. The method of claim 6 where the emulsion and the seawater mixture is maintained at a temperature above 250 F. for at least one hom.

8. The method of claim 6 where the ratio of 'emulsion to seawater is 3 to l.

9. A method` o transporting a Casmalia type crude oil from a lirst location to a second location comprising contacting at a rst location a type crude oil with water and a base in the presence of an emulsifying agent for the said crude oil, the ratio of said crude to said base being sodium hydroxide in a concentration of from 0.05 to 3.6 percent by weight based on total water, agitating the crude and the water to form an oil-in-water emulsion, moving the oilinwater emulsion through a pipeline from said first location to a second location, mixing the emulsion with seawater at a temperature in excess of 200 F. and in a ratio of emulsion to seawater of from betweenZ' to 1 to3y to l tobreaktheemulsionat said second location and separating the crude oil and e water.

10. The method of claim 9 where the emulsion is preheated to above 200 F. and the seawater is preheated to l2 above 175 F. prior to the mixlmeskabd toabout275 F. foratleastonehour. n Y

11. Themcthod of claim 9 where uptoprlttof the water used in the emulsion is ccproducedwas nier,

12. 'Ihe method of claim where a smallipatiyd treating chemical is added to the seawater.

13. A method uf transporting a Harbordt type ande oil from arst locatontoasecond contacting at a first location a Harbordt typ crude oil with wete'. and a base in the presence of an emnlsifyzg agent for the viscous crude oil, the ratio of siii cmde to said water being in the range of from 50/50 lo 70/ and the base being sodium hydroxide lin a am of about 0.10 by weight percent based on total water, agiiatingthecrude andthewater to formanoil-nwater emulsion, moving the oil-in-water emulri tireigh a pipeline from said first location o a second location, mixing the emulsion with seawater at a temperature in excess of 200 F. and in a ratio of emulsion h me: of from between 2 to l to 3% to l to break the emulsion at said second location and Separating the crude oil l and the water.

14. A method of tramporting viscous asphaltn crade oils through pipelines which comprises dispening 50 to 70 volumes of oil in 50 to 30 volumes of aqueous alkali having a normal concentration of 0H ion in the range about 0.2 to 1.5 normal to form an ol-in-water emnklon, passing the emulsion through the pipeline, withdrawing the emulsion from the pipeline and breaking the enmlon.

I References UNrrnn srArr-s rari-:Nrs '4 1.6mm 2/1921 Amm 25a-34s 1,841,413 3/1932 Pollock 252-345 3,006,354 1o/1961 sommer rs1-13v FOREIGN PATENTS 639,050 3.11962 canada. 625,980 8119s'. cms.

AIAN CoHAN, examiner flummfmlhlmmlm 

